WO2022245253A1 - Process for catalytically converting light hydrocarbon fractions and apparatus for carrying out same - Google Patents
Process for catalytically converting light hydrocarbon fractions and apparatus for carrying out same Download PDFInfo
- Publication number
- WO2022245253A1 WO2022245253A1 PCT/RU2022/050116 RU2022050116W WO2022245253A1 WO 2022245253 A1 WO2022245253 A1 WO 2022245253A1 RU 2022050116 W RU2022050116 W RU 2022050116W WO 2022245253 A1 WO2022245253 A1 WO 2022245253A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- heat exchangers
- catalytic
- recuperative heat
- gas
- kerosene
- Prior art date
Links
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 32
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 32
- 238000000034 method Methods 0.000 title claims abstract description 28
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 26
- 239000007789 gas Substances 0.000 claims abstract description 51
- 230000003197 catalytic effect Effects 0.000 claims abstract description 45
- 239000003350 kerosene Substances 0.000 claims abstract description 19
- 238000006243 chemical reaction Methods 0.000 claims abstract description 18
- 238000001816 cooling Methods 0.000 claims abstract description 17
- 238000010438 heat treatment Methods 0.000 claims abstract description 17
- 239000000203 mixture Substances 0.000 claims abstract description 14
- 239000012071 phase Substances 0.000 claims abstract description 13
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000007791 liquid phase Substances 0.000 claims abstract description 7
- 238000012545 processing Methods 0.000 claims description 35
- 239000002994 raw material Substances 0.000 claims description 28
- 238000009434 installation Methods 0.000 claims description 27
- 239000003054 catalyst Substances 0.000 claims description 17
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 8
- 229910021536 Zeolite Inorganic materials 0.000 claims description 5
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 5
- 239000010457 zeolite Substances 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 3
- 239000000377 silicon dioxide Substances 0.000 claims description 3
- 239000002737 fuel gas Substances 0.000 claims description 2
- 239000012467 final product Substances 0.000 claims 2
- 239000000047 product Substances 0.000 abstract description 7
- 238000006555 catalytic reaction Methods 0.000 abstract description 6
- 239000007795 chemical reaction product Substances 0.000 abstract description 3
- 239000003208 petroleum Substances 0.000 abstract description 2
- 239000003502 gasoline Substances 0.000 description 14
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 7
- 230000015572 biosynthetic process Effects 0.000 description 6
- 150000003464 sulfur compounds Chemical class 0.000 description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 238000005899 aromatization reaction Methods 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 238000003786 synthesis reaction Methods 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 150000001338 aliphatic hydrocarbons Chemical class 0.000 description 3
- 150000001336 alkenes Chemical class 0.000 description 3
- 230000033228 biological regulation Effects 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 125000001931 aliphatic group Chemical group 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012263 liquid product Substances 0.000 description 2
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000011541 reaction mixture Substances 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 102200118166 rs16951438 Human genes 0.000 description 2
- 239000004071 soot Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 230000006641 stabilisation Effects 0.000 description 2
- 238000011105 stabilization Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 150000001491 aromatic compounds Chemical class 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000007036 catalytic synthesis reaction Methods 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- NCGDAXSZZUDOCZ-UHFFFAOYSA-N ethene;sulfane Chemical compound S.C=C NCGDAXSZZUDOCZ-UHFFFAOYSA-N 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 150000002898 organic sulfur compounds Chemical class 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000002028 premature Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G35/00—Reforming naphtha
- C10G35/04—Catalytic reforming
- C10G35/06—Catalytic reforming characterised by the catalyst used
- C10G35/095—Catalytic reforming characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/305—Octane number, e.g. motor octane number [MON], research octane number [RON]
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/06—Gasoil
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Definitions
- the group of inventions relates to the processing of various petroleum feedstocks, namely to complex devices for the production of a component of high-octane gasoline and aromatic hydrocarbons by catalytic processing of light hydrocarbon fractions and can be used both at production facilities and primary processing of hydrocarbon feedstocks, and in independent operation.
- a known method for the catalytic processing of light hydrocarbon fractions (patent CIIIAN 5030783, IPC C07C 1/04, publ. 07/1991), which is carried out by contacting the raw material with a zeolite catalyst in the reaction zone, in which the heat necessary to maintain the aromatization reaction of at least part of the raw material , is directly transferred from the hot flue gas, which contains practically no oxygen, obtained by burning hydrogen-deficient fuel.
- Aromatic hydrocarbons, C3-C5 aliphatic hydrocarbons (recycle stream) and a mixture of CO, CO2 and H2 (synthesis gas) are separated from the product stream.
- the synthesis gas is sent to the Fischer-Tropsch synthesis or to the synthesis of methanol, and the resulting products can be used to produce liquid hydrocarbons in the main reactor.
- the disadvantage of this method is the use of flue gases as a regenerating gas and the need to clean it from soot, which is inevitably formed during the combustion of hydrocarbon gas, which reduces the efficiency of processing.
- SUBSTITUTE SHEET (RULE 26) hydrocarbons to aromatics.
- the aromatization reaction (the reaction of formation of aromatic hydrocarbons from aliphatic ones) is carried out by overheating the feedstock, and the problem of increasing the yield of aromatic hydrocarbons by recycling aliphatic hydrocarbons C 2-C4 and C5 + is solved, while the catalyst is contacted with a mixture of feedstock and recycles.
- the disadvantage of this method is the intensive mixing of the reaction mixture along the reactor, leading to high energy consumption.
- a known method for the catalytic processing of light hydrocarbon fractions (according to the patent of the Russian Federation N ° 2181750, IPC C10G 35/095, publ. 19.04.2001, prototype), according to which the petroleum distillate with a boiling point not exceeding 400 ° C, containing sulfur compounds in quantities of not more than 10 wt.% in terms of elemental sulfur, at a temperature of 250-550 ° C, a pressure of not more than 2 MPa and a mass flow rate of raw materials of not more than 10 h no more than 450, selected from the range: ZSM-5, ZSM-11, ZSM-35, ZSM-38, ZSM-48, BETA.
- Known catalytic plant for the processing of light hydrocarbon fractions to increase their octane number which contains a furnace for heating and evaporating raw materials, adiabatic catalytic reactors for chemical conversion of raw materials, distillation columns for stabilizing the raw materials and isolating the target product and technologically connected with them heat exchangers, radiators cooling, condensers and separators.
- the units for fractionation of raw materials and reaction products operate in a continuous mode, and the reactors in the "reaction-regeneration" mode (RF patent JVb 2098173, IPC C10G 35/04, publ. 10.12.1997).
- a known installation for the catalytic processing of aliphatic hydrocarbons C2-C12 into aromatic hydrocarbons or high-octane gasoline (RF patent JVb 2175959, MIK C07C 1/00, C07C 2/02, C07C 2/76, C07C 15/00, publ. 20.11.2001, prototype).
- the installation contains a reactor, a furnace, heat exchangers, cooling radiators, separators and a stabilization column connected by pipelines. Carrying out the aromatization reaction of C2-C4 hydrocarbons on the first shelf of the reactor leads to the formation of aromatic products C6-C10, which then enter the second shelf of the reactor, where straight-run gasoline is converted.
- the task to be solved by the inventions is to increase the efficiency and quality of processing of gasoline and multicomponent raw materials.
- the technical result is an increase in the efficiency of processing light hydrocarbon fractions into a high-quality catalyzate.
- the technical result is achieved in the proposed method for the catalytic processing of light hydrocarbon fractions, which includes heating the feedstock, separating it into kerosene fractions and a feed gas mixture, which is heated and sent to the reaction zone for contact with the catalyst in
- SUBSTITUTE SHEET (RULE 26) conditions of direct conversion, removal of the catalyzate from the reaction zone, its cooling by supplying it for circulation first to the system of heating recuperative heat exchangers, and subsequent separation of the catalyzate into a gas phase containing hydrogen sulfide and a liquid phase.
- the conditions for carrying out the direct conversion process are temperature from 350 to 450 ° C and pressure from 3.5 to 5 atm, space velocity of the feedstock - from 4.5 to 5.0 liters per minute .
- the technical result is achieved in the proposed installation for the catalytic processing of light hydrocarbon fractions, which contains heating and cooling heat exchangers connected by pipelines, a furnace and a catalytic reactor, the catalysate outlet from which is connected through cooling heat exchangers to a gas separator separating the catalyzate into a gas phase containing hydrogen sulfide and a liquid phase.
- the outlet of the heating recuperative heat exchangers is connected to a kerosene separator configured to separate the heated feedstock into a gas feed mixture intended for subsequent entry into the catalytic reactor and kerosene fractions.
- the gas phase outlet of the gas separator is connected by a pipeline to the furnace, and the catalysate outlet from the reactor is connected to a system of heating recuperative heat exchangers.
- SUBSTITUTE SHEET (RULE 26) octane number.
- the sulfur concentration decreases up to 12 times.
- straight-run gasoline after catalysis becomes a highly liquid product.
- a great advantage of the process of direct conversion of hydrocarbons is its resistance to sulfur compounds, always in one or another concentration, present in oil and gas condensate.
- Organosulfur compounds of raw materials are converted into paraffinic, aromatic hydrocarbons and hydrogen sulfide as a result of successive reactions.
- the first of these are the reactions of breaking the C-S bonds of mercaptans, sulfides, thiophanes and their derivatives, as a result of which molecules of hydrogen sulfide and intermediate olefins are formed, for example, similarly to the schemes: ethylene hydrogen sulfide
- the resulting olefins are further converted into paraffinic and aromatic hydrocarbons, and hydrogen sulfide is separated together with the by-products of the process - C1-C4 hydrocarbons - from liquid products at the stages of separation and stabilization to obtain desulfurized gasoline.
- the proposed method and installation provide automatic maintenance of the specified parameters of catalytic processing using controllers, by supplying control signals to pumps and electromagnetic valves, based on readings from temperature sensors, pressure sensors, float sensors and flow meters.
- the proposed method and device provide efficient processing of light hydrocarbon distillates into high-quality
- SUBSTITUTE SHEET (RULE 26) b catalysate with a low sulfur content without a preliminary process of desulfurization and dehydration of the feedstock.
- figure 1 shows a schematic flow diagram of the installation for the catalytic processing of light hydrocarbon feedstock.
- the installation for the catalytic processing of light hydrocarbon feedstock (naphtha, nefras, straight-run gasoline, BGS) into a high-quality catalyzate with the parameters of A-80 gasoline contains (Fig. 1) a furnace 1 connected by a pipeline to a catalytic reactor 2, a system of heating recuperative heat exchangers 3, 4, 5 and a system of cooling heat exchangers 6, 7, 8, 9, including a pipe heat exchanger 6 installed at the outlet of the reactor 2, two recuperative heat exchangers 7 and 8 connected to cooling radiators 10, and a recuperative heat exchanger 9 through which industrial water passes for cooling .
- the catalytic reactor 2 as shown in the present embodiment, consists of two reactor columns R-1 and R 2.
- the outlet of the catalyzate from the catalytic reactor 2 is connected through a system of heat exchangers 6, 5, 4, 3, 7, 8, 9 with a gas separator 11, configured to separate the catalyzate into a gas phase and a liquid phase, which is high-octane gasoline.
- the gas phase contains hydrogen sulfide gas formed by light sulfur compounds after the separation of the catalyzate in the gas separator 11, which is subsequently burned in the feedstock heating furnace 1.
- the outlet of the system of heating heat exchangers 3, 4, 5 is connected to a kerosene separator 12, which, in turn, is connected through a recuperative heat exchanger 13 to a container 14 for collecting kerosene.
- the device To stabilize the raw material feed rate, the device is provided with a raw material accumulation tank 15, at the inlet of which a recuperative heat exchanger 16 is installed.
- the level of the accumulated working fluid in tanks 14 and 15 is controlled using float sensors installed in them (not shown).
- Regulation of the speed of passage of the working medium is provided by pumps 17, 18, 19, 20 and control valves 21, 22, 23. raw materials to the installation, the pump 19 provides regulation of the output of kerosene from the installation, the pump 20 provides regulation of the output of the catalyzate. To prevent the flow of the working medium in the opposite direction, check valves 24, 25, 26, 27 are provided in the installation.
- the control of the speed of the passage of the working fluid is carried out using installed flow meters: at the input of raw materials to the installation - 28, at the outlet of catalyzate - 29, at the outlet of kerosene - 30.
- filters 31 and 32 are provided, installed at the inlet of raw materials to the installation and at the outlet of the catalyzate from the heat exchanger system.
- Temperature control is carried out using temperature sensors (not shown) installed in the furnace 1 and in the columns of the reactor 2.
- the composition of light fractions of unstable gas condensate includes low molecular weight mercaptans.
- the reactor 2 of the installation Before starting work, the reactor 2 of the installation is heated to a temperature of 350°C using electric heaters. After the reactor 2 reaches the required temperature, pumps 17, 18 are turned on and the feedstock is fed into the furnace 1, where it is heated by a diesel burner (at the time of start-up) connected to an external source of diesel fuel.
- the indicator of the output of the installation in the operating mode is the constant release of gas on the candle is lived out and the pressure in the reactor 2 rises to the operating one. After that, the operation of the installation switches to the mode of operation of heating the raw material with
- Raw material - straight-run gasoline fraction KK-210°C is supplied by pump 17 through filter 31 and recuperative heat exchanger 16 into raw material storage tank 15 and then by pump 18 it is driven through a system of recuperative heat exchangers 13, 3, 4 and 5, where it is heated by the heat of reaction products to 200°C is sent to the kerosene separator 12, in which from the top of the separator 12 the gas mixture is sent through the pipe heat exchanger 6 to the furnace 1 for heating, and from the bottom of the separator 12 the kerosene fractions that have passed through the heat exchanger 13 are collected into the tank 14 for the accumulation of kerosene, which are further pump 19 is pumped out of the installation.
- the heated gas mixture enters the catalytic reactor 2 filled with a high-silica zeolite-containing catalyst.
- the volumetric feed rate of raw materials is from 4.5 to 5.0 liters per minute.
- reactor 2 at a temperature of 350-450°C and a pressure of 3.5 to 5 atm, the process of converting low-octane components of straight-run gasoline fractions into high-octane ones is carried out due to catalytic isomerization and aromatization of paraffins and dehydrogenation of naphthenic hydrocarbons.
- the reaction mixture passes with a uniform drop through the pipelines of the reactor 2, in which the catalyst is filled, where with the passage of characteristic chemical reactions that transform the hydrocarbon composition of gasoline fractions.
- the reactions proceed in one step with the absorption of heat and the release of an excess amount of hydrogen-containing gases (HCG).
- HCG hydrogen-containing gases
- the adsorption purification of the gas mixture from sulfur compounds occurs, which remain in the reactor and are removed from it at the time of regeneration (during the catalytic oxidation reaction).
- the process is carried out in a fixed catalyst bed in a single pass mode, that is, without the recycle flow of aromatic compounds; the olefin stream is mainly consumed in the reaction.
- the zeolite-based catalyst used other than
- the resulting catalyzate is fed back for circulation to the system of heat exchangers 6, 5, 4, 3, and then through 7, 8, 9, where it is cooled to a temperature of up to 25°C, after which it enters the gas separator 11 through the filter 32 of the catalyzate.
- the balance excess of hydrocarbon gas is removed from the plant and used as fuel gas for the furnace 1.
- the catalyzate from the bottom of the gas separator 11 is pumped out by the pump 20 through the heat exchanger 16 to the tank farm.
- catalysis gasoline (because 30-208 ° C) (OCMM 74-80) was obtained, which is used as a component for the production of motor gasoline.
- the installation automatically maintains the parameters of the technological mode at a given level, registers the parameters and signals about the deviation of the parameters from the specified values.
- Maintaining the set parameters is achieved by reading controllers readings from temperature sensors installed in furnace 1 and reactor 2, pressure sensors installed in reactor 2, float sensors installed in tanks 14 and 15, flow meters 28, 29, 30 and control of electromagnetic valves 21, 22, 23 on the installation pipelines.
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Crystallography & Structural Chemistry (AREA)
- Materials Engineering (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The inventions relate to the conversion of various petroleum feedstocks. A first invention relates to an apparatus for catalytically converting light hydrocarbon fractions, which comprises, connected in sequence by pipelines, recuperative heat exchangers (3, 4, 5) for heating feedstock, a furnace (1), and a catalytic reactor (2), as well as recuperative heat exchangers (7, 8, 9) for cooling catalysis products, said heat exchangers being connected to a gas separator (11) capable of separating the catalysis products into a hydrogen sulphide-containing gas phase and a liquid phase that is the end product of the catalytic conversion. The outlet of recuperative heat exchangers (3, 4, 5) is connected to a kerosene separator (12) capable of separating the heated feedstock into a feedstock gas mixture, to be sent to the catalytic reactor (2), and a kerosene fraction, wherein a gas phase outlet of the gas separator (11) is connected by a pipeline to the furnace (1), and a catalysis product outlet of the catalytic reactor (2) is connected to recuperative heat exchangers (6, 5, 4, 3), which are connected to the cooling heat exchangers (7, 8, 9). A second invention relates to a process for catalytically converting light hydrocarbon fractions. The technical result is more efficient conversion of light hydrocarbon fractions.
Description
Способ каталитической переработки легких углеводородных фракций и установка для его осуществления Method for catalytic processing of light hydrocarbon fractions and installation for its implementation
Область техники Technical field
Группа изобретений относится к переработке различного нефтяного сырья, а именно к комплексным устройствам для производства компонента высокооктанового бензина и ароматических углеводородов путем каталитической переработки легких углеводородных фракций и может быть использована как на объектах добычи и первичной переработки углеводородного сырья, так и в самостоятельной эксплуатации. The group of inventions relates to the processing of various petroleum feedstocks, namely to complex devices for the production of a component of high-octane gasoline and aromatic hydrocarbons by catalytic processing of light hydrocarbon fractions and can be used both at production facilities and primary processing of hydrocarbon feedstocks, and in independent operation.
Уровень техники State of the art
Известен способ каталитической переработки легких углеводородных фракций (патент CIIIAN 5030783, МПК С07С 1/04, публ. 09.07.1991), который осуществляется при контакте сырья с цеолитным катализатором в зоне реакции, при котором тепло, необходимое для поддержания реакции ароматизации хотя бы части сырья, непосредственно передается от горячего топочного газа, практически не содержащего кислорода, полученного при сжигании водорододефицитного топлива. Из потока продуктов выделяют ароматические углеводороды, С3-С5 алифатические углеводороды (рецикловый поток) и смесь СО, СО2 и Н2 (синтез-газ). Синтез-газ направляют на синтез Фишера-Тропша или на синтез метанола, причем полученные продукты могут быть использованы для получения жидких углеводородов в основном реакторе. A known method for the catalytic processing of light hydrocarbon fractions (patent CIIIAN 5030783, IPC C07C 1/04, publ. 07/09/1991), which is carried out by contacting the raw material with a zeolite catalyst in the reaction zone, in which the heat necessary to maintain the aromatization reaction of at least part of the raw material , is directly transferred from the hot flue gas, which contains practically no oxygen, obtained by burning hydrogen-deficient fuel. Aromatic hydrocarbons, C3-C5 aliphatic hydrocarbons (recycle stream) and a mixture of CO, CO2 and H2 (synthesis gas) are separated from the product stream. The synthesis gas is sent to the Fischer-Tropsch synthesis or to the synthesis of methanol, and the resulting products can be used to produce liquid hydrocarbons in the main reactor.
Недостатком способа является использование дымовых газов в качестве регенерирующего газа и необходимость очистки его от сажи, которая неизбежно образуется при сжигании углеводородного газа, что снижает эффективность переработки. The disadvantage of this method is the use of flue gases as a regenerating gas and the need to clean it from soot, which is inevitably formed during the combustion of hydrocarbon gas, which reduces the efficiency of processing.
Известен способ каталитической переработки легких углеводородных фракций (патент США N 4996381, МПК С07С 15/00, публ. 26.02.1991), включающий основные операции процесса переработки алифатических A known method for the catalytic processing of light hydrocarbon fractions (US patent N 4996381, IPC S07S 15/00, publ. 26.02.1991), including the main operations of the processing of aliphatic
ЗАМЕНЯЮЩИЙ ЛИСТ (ПРАВИЛО 26)
углеводородов в ароматические. В этом способе реакцию ароматизации (реакцию образования ароматических углеводородов из алифатических) осуществляют, перегревая сырье, и решают задачу повышения выхода ароматических углеводородов рециклом алифатических углеводородов С 2- С4 и С5+, при этом осуществляют контакт катализатора со смесью сырья и рециклов. SUBSTITUTE SHEET (RULE 26) hydrocarbons to aromatics. In this method, the aromatization reaction (the reaction of formation of aromatic hydrocarbons from aliphatic ones) is carried out by overheating the feedstock, and the problem of increasing the yield of aromatic hydrocarbons by recycling aliphatic hydrocarbons C 2-C4 and C5 + is solved, while the catalyst is contacted with a mixture of feedstock and recycles.
Недостатком известного способа является интенсивное перемешивание реакционной смеси вдоль реактора, приводящее к высоким энергозатратам. The disadvantage of this method is the intensive mixing of the reaction mixture along the reactor, leading to high energy consumption.
Известен способ каталитической переработки легких углеводородных фракций (по патенту РФ N° 2181750, МПК C10G 35/095, публ. 19.04.2001, прототип), согласно которому нефтяной дистиллят с температурой кипения не вьтттте 400°С, содержащий соединения серы в количествах не более 10 мас.% в пересчете на элементарную серу, при температуре 250-550°С, давлении не более 2 МПа и массовом расходе сырья не более 10 ч 1 контактируют с пористым катализатором, в качестве которого используют цеолит алюмосиликатного состава с мольным отношением SiCh/AhCb не более 450, выбранный из ряда: ZSM-5, ZSM-11, ZSM-35, ZSM- 38, ZSM-48, BETA. A known method for the catalytic processing of light hydrocarbon fractions (according to the patent of the Russian Federation N ° 2181750, IPC C10G 35/095, publ. 19.04.2001, prototype), according to which the petroleum distillate with a boiling point not exceeding 400 ° C, containing sulfur compounds in quantities of not more than 10 wt.% in terms of elemental sulfur, at a temperature of 250-550 ° C, a pressure of not more than 2 MPa and a mass flow rate of raw materials of not more than 10 h no more than 450, selected from the range: ZSM-5, ZSM-11, ZSM-35, ZSM-38, ZSM-48, BETA.
Недостатком известного способа является необходимость предварительного обессеривания сырья, что в значительной мере осложняет процесс переработки углеводородного сырья. The disadvantage of this method is the need for preliminary desulfurization of raw materials, which greatly complicates the process of processing hydrocarbon raw materials.
Известна каталитическая установка переработки легких углеводородных фракций для повышения их октанового числа, которая содержит печь для нагрева и испарения сырья, каталитические реакторы адиабатического типа для осуществления химического превращения сырья, ректификационные колонны для стабилизации исходного сырья и выделения целевого продукта и технологически обвязанные с ними теплообменники, радиаторы охлаждения, конденсаторы и сепараторы. Узлы фракционирования сырья и продуктов реакции работают в непрерывном режиме, а реакторы в режиме "реакция-регенерация" (патент РФ JVb 2098173, МПК C10G 35/04, публ. 10.12.1997 г.). Known catalytic plant for the processing of light hydrocarbon fractions to increase their octane number, which contains a furnace for heating and evaporating raw materials, adiabatic catalytic reactors for chemical conversion of raw materials, distillation columns for stabilizing the raw materials and isolating the target product and technologically connected with them heat exchangers, radiators cooling, condensers and separators. The units for fractionation of raw materials and reaction products operate in a continuous mode, and the reactors in the "reaction-regeneration" mode (RF patent JVb 2098173, IPC C10G 35/04, publ. 10.12.1997).
ЗАМЕНЯЮЩИЙ ЛИСТ (ПРАВИЛО 26)
Основными недостатками установки являются сложность технологической схемы и относительно высокие потери в расчете на сырье. Кроме того, использование дымовых газов в качестве регенерирующего газа и необходимость очистки его от сажи, которая неизбежно образуется при сжигании углеводородного газа, требует установки дорогих фильтров тонкой очистки, а также ведет к снижению активности катализатора при его регенерации. Кроме того, использование ректификационной колонны усложняет технологический процесс. SUBSTITUTE SHEET (RULE 26) The main disadvantages of the installation are the complexity of the technological scheme and relatively high losses in terms of raw materials. In addition, the use of flue gases as a regenerating gas and the need to clean it from soot, which is inevitably formed during the combustion of hydrocarbon gas, requires the installation of expensive fine filters, and also leads to a decrease in catalyst activity during its regeneration. In addition, the use of a distillation column complicates the process.
Известна установка каталитичекой переработки алифатических углеводородов С2-С12 в ароматические углеводороды или высокооктановый бензин (патент РФ JVb 2175959, МИК С07С 1/00, С07С 2/02, С07С 2/76, С07С 15/00, публ. 20.11.2001 г., прототип). Установка содержит реактор, печь, теплообменники, радиаторы охлаждения, сепараторы и стабилизационную колонну, соединенные трубопроводами. Проведение реакции ароматизации углеводородов С2-С4 на первой полке реактора ведет к образованию ароматических продуктов С6-С10, которые затем поступают на вторую полку реактора, где превращают прямогонный бензин. A known installation for the catalytic processing of aliphatic hydrocarbons C2-C12 into aromatic hydrocarbons or high-octane gasoline (RF patent JVb 2175959, MIK C07C 1/00, C07C 2/02, C07C 2/76, C07C 15/00, publ. 20.11.2001, prototype). The installation contains a reactor, a furnace, heat exchangers, cooling radiators, separators and a stabilization column connected by pipelines. Carrying out the aromatization reaction of C2-C4 hydrocarbons on the first shelf of the reactor leads to the formation of aromatic products C6-C10, which then enter the second shelf of the reactor, where straight-run gasoline is converted.
Недостатки известной установки - недостаточно высокая эффективность её работы по причине использования сложного ректификационного оборудования. Сложная конструкция реактора создает трудности при загрузке и выгрузке катализатора. The disadvantages of the known installation is not enough high efficiency of its work due to the use of complex distillation equipment. The complex design of the reactor makes it difficult to load and unload the catalyst.
Раскрытие изобретений Disclosure of inventions
Задачей, на решение которой направлены изобретения, является повышение эффективности и качества переработки бензинового и многокомпонентного сырья. The task to be solved by the inventions is to increase the efficiency and quality of processing of gasoline and multicomponent raw materials.
Технический результат - повышение эффективности переработки легких углеводородных фракций в качественный катализат. The technical result is an increase in the efficiency of processing light hydrocarbon fractions into a high-quality catalyzate.
Технический результат достигается в предложенном способе каталитической переработки легких углеводородных фракций, включающем нагрев сырья, его разделение на керосиновые фракции и газосырьевую смесь, которую нагревают и направляют в зону реакции, для контакта с катализатором в The technical result is achieved in the proposed method for the catalytic processing of light hydrocarbon fractions, which includes heating the feedstock, separating it into kerosene fractions and a feed gas mixture, which is heated and sent to the reaction zone for contact with the catalyst in
ЗАМЕНЯЮЩИЙ ЛИСТ (ПРАВИЛО 26)
условиях прямой конверсии, вывод катализата из зоны реакции, его охлаждение, путем подачи на циркуляцию сначала в систему разогревающих рекуперативных теплообменников, и последующее разделение катализата на газовую фазу, содержащую сероводород, и жидкую фазу. SUBSTITUTE SHEET (RULE 26) conditions of direct conversion, removal of the catalyzate from the reaction zone, its cooling by supplying it for circulation first to the system of heating recuperative heat exchangers, and subsequent separation of the catalyzate into a gas phase containing hydrogen sulfide and a liquid phase.
При этом в процессе прямого катализа происходит газофазное превращение низкооктановых компонентов в высокооктановые с поглощением тепла, выделением избыточного количества водородосодержащих газов и адсорбционной очисткой газосырьевой смеси от сернистых соединений. Что немаловажно, поскольку в процессе переработки легкого углеводородного сырья растет необходимость удаления соединений серы, потому что сера вызывает коррозию трубопроводного, нагнетающего и перерабатывающего оборудования, отравление катализаторов, применяемых при переработке и сжигании ископаемых топлив, и преждевременное разрушение двигателей сгорания. В частности, при использовании качестве катализатора высококремнеземного цеолитосодержащего катализатора условиями для осуществления процесса прямой конверсии являются температура от 350 до 450°С и давление от 3,5 до 5 атм, объемная скорость подачи сырья - от 4,5 до 5,0 литров в минуту. At the same time, in the process of direct catalysis, a gas-phase transformation of low-octane components into high-octane components occurs with the absorption of heat, the release of an excess amount of hydrogen-containing gases, and the adsorption purification of the gas mixture from sulfur compounds. This is important, as the need to remove sulfur compounds increases in the processing of light hydrocarbon feedstock, because sulfur causes corrosion of pipeline, injection and processing equipment, poisoning of catalysts used in the processing and combustion of fossil fuels, and premature destruction of combustion engines. In particular, when a high-silica zeolite-containing catalyst is used as a catalyst, the conditions for carrying out the direct conversion process are temperature from 350 to 450 ° C and pressure from 3.5 to 5 atm, space velocity of the feedstock - from 4.5 to 5.0 liters per minute .
Технический результат достигается в предложенной установке каталитической переработки легких углеводородных фракций, которая содержит связанные трубопроводами разогревающие и охлаждающие теплообменники, печь и каталитический реактор, выход катализата из которого через охлаждающие теплообменники соединен с газосепаратором, разделяющим катализат на газовую фазу, содержащую сероводород, и жидкую фазу. При этом выход разогревающих рекуперативных теплообменников соединен с керосиновым сепаратором, выполненным с возможностью разделения разогретого сырья на газосырьевую смесь, предназначенную для последующего поступления в каталитический реактор, и керосиновые фракции. При этом выход газовой фазы газосепаратора связан трубопроводом с печью, а выход катализата из реактора связан с системой разогревающих рекуперативных теплообменников. The technical result is achieved in the proposed installation for the catalytic processing of light hydrocarbon fractions, which contains heating and cooling heat exchangers connected by pipelines, a furnace and a catalytic reactor, the catalysate outlet from which is connected through cooling heat exchangers to a gas separator separating the catalyzate into a gas phase containing hydrogen sulfide and a liquid phase. At the same time, the outlet of the heating recuperative heat exchangers is connected to a kerosene separator configured to separate the heated feedstock into a gas feed mixture intended for subsequent entry into the catalytic reactor and kerosene fractions. In this case, the gas phase outlet of the gas separator is connected by a pipeline to the furnace, and the catalysate outlet from the reactor is connected to a system of heating recuperative heat exchangers.
При работе в установке происходят химические процессы, которые кардинально меняют фракционный состав и внешний вид сырья, его запах и When working in the plant, chemical processes occur that radically change the fractional composition and appearance of the raw material, its smell and
ЗАМЕНЯЮЩИЙ ЛИСТ (ПРАВИЛО 26)
октановое число. Концентрация серы уменьшается до 12 раз. В результате прямогонный бензин после катализа становится высоколиквидным продуктом. SUBSTITUTE SHEET (RULE 26) octane number. The sulfur concentration decreases up to 12 times. As a result, straight-run gasoline after catalysis becomes a highly liquid product.
Большим достоинством процесса прямой конверсии углеводородов является его стойкость к сернистым соединениям, всегда в той или иной концентрации, присутствующих в нефти и газовом конденсате. Сероорганические соединения сырья превращаются в парафиновые, ароматические углеводороды и сероводород в результате последовательно протекающих реакций. Первыми из них являются реакции разрыва С-S связи меркаптанов, сульфидов, тиофанов и их производных, в результате протекания которых образуются молекулы сероводорода и промежуточных олефинов, например, аналогично схемам: C4H9SH С4Н8 + H2S бутилмеркаптан бутилен сероводород (CH3)2S С2Н4 + H2S диметилсульфид этилен сероводород A great advantage of the process of direct conversion of hydrocarbons is its resistance to sulfur compounds, always in one or another concentration, present in oil and gas condensate. Organosulfur compounds of raw materials are converted into paraffinic, aromatic hydrocarbons and hydrogen sulfide as a result of successive reactions. The first of these are the reactions of breaking the C-S bonds of mercaptans, sulfides, thiophanes and their derivatives, as a result of which molecules of hydrogen sulfide and intermediate olefins are formed, for example, similarly to the schemes: ethylene hydrogen sulfide
Образовавшиеся олефины далее превращаются в парафиновые и ароматические углеводороды, а сероводород отделяется вместе с побочными продуктами процесса - углеводородами С1-С4 - от жидких продуктов на стадиях сепарации и стабилизации с получением обессеренного бензина. The resulting olefins are further converted into paraffinic and aromatic hydrocarbons, and hydrogen sulfide is separated together with the by-products of the process - C1-C4 hydrocarbons - from liquid products at the stages of separation and stabilization to obtain desulfurized gasoline.
Кроме того, использование в предлагаемом способе и устройстве для охлаждения катализата системы разогревающих рекуперативных теплообменников, а также нагрев сырья газом, выделяемым в ходе реакции, повышает КПД установки до 90%. Возможно также использование излишков газа для электрогенерации или систем отопления. In addition, the use of a system of heating recuperative heat exchangers in the proposed method and device for cooling the catalyzate, as well as heating the raw material with the gas released during the reaction, increases the efficiency of the installation up to 90%. It is also possible to use excess gas for power generation or heating systems.
Кроме того, предлагаемые способ и установка обеспечивают автоматическое поддержание заданных параметров каталитической переработки с помощью контроллеров, путем подачи управляющих сигналов на насосы и электромагнитные клапаны, на основании считываемых показаний с температурных датчиков, датчиков давления, поплавковых датчиков и расходомеров. In addition, the proposed method and installation provide automatic maintenance of the specified parameters of catalytic processing using controllers, by supplying control signals to pumps and electromagnetic valves, based on readings from temperature sensors, pressure sensors, float sensors and flow meters.
Таким образом, предлагаемые способ и устройство обеспечивают эффективную переработку легких углеводородных дистиллятов в качественный Thus, the proposed method and device provide efficient processing of light hydrocarbon distillates into high-quality
ЗАМЕНЯЮЩИЙ ЛИСТ (ПРАВИЛО 26)
б катализат с низким содержанием серы без предварительного процесса обессеривания и обезвоживания сырья. SUBSTITUTE SHEET (RULE 26) b catalysate with a low sulfur content without a preliminary process of desulfurization and dehydration of the feedstock.
Краткое описание чертежей Brief description of the drawings
Установка поясняется описанием конкретного примера выполнения и прилагаемыми графическими материалами, где на фиг.1 изображена принципиальная технологическая схема установки каталитической переработки легкого углеводородного сырья. The installation is explained by the description of a specific example of execution and the attached graphics, where figure 1 shows a schematic flow diagram of the installation for the catalytic processing of light hydrocarbon feedstock.
Осуществление изобретений Implementation of inventions
Установка каталитической переработки легкого углеводородного сырья (нафта, нефрас, прямогонный бензин, бгс) в качественный катализат с параметрами бензина А-80 содержит (фиг. 1) печь 1, связанную трубопроводом с каталитическим реактором 2, систему разогревающих рекуперативных теплообменников 3, 4, 5 и систему охлаждающих теплообменников 6, 7, 8, 9, в числе которых трубный теплообменник 6, установленный на выходе реактора 2, два рекуперативных теплообменника 7 и 8, связанных с радиаторами охлаждения 10, и рекуперативный теплообменник 9, через который для охлаждения проходит производственная вода. The installation for the catalytic processing of light hydrocarbon feedstock (naphtha, nefras, straight-run gasoline, BGS) into a high-quality catalyzate with the parameters of A-80 gasoline contains (Fig. 1) a furnace 1 connected by a pipeline to a catalytic reactor 2, a system of heating recuperative heat exchangers 3, 4, 5 and a system of cooling heat exchangers 6, 7, 8, 9, including a pipe heat exchanger 6 installed at the outlet of the reactor 2, two recuperative heat exchangers 7 and 8 connected to cooling radiators 10, and a recuperative heat exchanger 9 through which industrial water passes for cooling .
Каталитический реактор 2, как показано в представленном примере осуществления, состоит из двух реакторных колонн Р-1 и Р 2. The catalytic reactor 2, as shown in the present embodiment, consists of two reactor columns R-1 and R 2.
Выход катализата из каталитического реактора 2 соединен через систему теплообменников 6, 5, 4, 3, 7, 8, 9 с газосепаратором 11, выполненным с возможностью разделения катализата на газовую фазу и жидкую фазу, являющуюся высокооктановым бензином. Газовая фаза содержит сероводородный газ, образованный легкими соединениями серы после разделения катализата в газосепараторе 11, который в дальнейшем сжигается в печи 1 нагрева сырья. The outlet of the catalyzate from the catalytic reactor 2 is connected through a system of heat exchangers 6, 5, 4, 3, 7, 8, 9 with a gas separator 11, configured to separate the catalyzate into a gas phase and a liquid phase, which is high-octane gasoline. The gas phase contains hydrogen sulfide gas formed by light sulfur compounds after the separation of the catalyzate in the gas separator 11, which is subsequently burned in the feedstock heating furnace 1.
Выход системы разогревающих теплообменников 3, 4, 5 соединен с керосиновым сепаратором 12, который в свою очередь через рекуперативный теплообменник 13 связан с емкостью 14 для сбора керосина. The outlet of the system of heating heat exchangers 3, 4, 5 is connected to a kerosene separator 12, which, in turn, is connected through a recuperative heat exchanger 13 to a container 14 for collecting kerosene.
ЗАМЕНЯЮЩИЙ ЛИСТ (ПРАВИЛО 26)
Для стабилизации скорости подачи сырья устройстве предусмотрена емкость накопления сырья 15, на входе которой установлен рекуперативный теплообменник 16. Контроль уровня накопленной рабочей жидкости в емкостях 14 и 15 контролируется с помощью установленных в них поплавковых датчиках (не показаны). SUBSTITUTE SHEET (RULE 26) To stabilize the raw material feed rate, the device is provided with a raw material accumulation tank 15, at the inlet of which a recuperative heat exchanger 16 is installed. The level of the accumulated working fluid in tanks 14 and 15 is controlled using float sensors installed in them (not shown).
Регулирование скорости прохождения рабочей среды обеспечивается с помощью насосов 17, 18, 19, 20 и регулировочных вентилей 21, 22, 23. Установленные насосы 17, 18, 19, 20 обеспечивают регулирование скорости прохождения рабочей среды: насосы входа сырья 17, 18 обеспечивают регулирование подачи сырья на установку, насос 19 обеспечивает регулирование выхода керосина из установки, насос 20 обеспечивает регулирование выхода катализата. Для предотвращения движения потока рабочей среды в противоположном направлении в установке предусмотрены обратные клапаны 24, 25, 26, 27. Regulation of the speed of passage of the working medium is provided by pumps 17, 18, 19, 20 and control valves 21, 22, 23. raw materials to the installation, the pump 19 provides regulation of the output of kerosene from the installation, the pump 20 provides regulation of the output of the catalyzate. To prevent the flow of the working medium in the opposite direction, check valves 24, 25, 26, 27 are provided in the installation.
Контроль скорости прохождения рабочей жидкости осуществляется с помощью установленных расходомеров: на входе сырья в установку - 28, на выходе катализата - 29, на выходе керосина - 30. The control of the speed of the passage of the working fluid is carried out using installed flow meters: at the input of raw materials to the installation - 28, at the outlet of catalyzate - 29, at the outlet of kerosene - 30.
Для очистки потока рабочей жидкости предусмотрены фильтры 31 и 32, установленные на входе сырья в установку и на выходе катализата из системы теплообменников. To clean the flow of the working fluid, filters 31 and 32 are provided, installed at the inlet of raw materials to the installation and at the outlet of the catalyzate from the heat exchanger system.
Контроль температуры осуществляется с помощью температурных датчиков (не показаны), установленных в печи 1 и в колоннах реактора 2. Temperature control is carried out using temperature sensors (not shown) installed in the furnace 1 and in the columns of the reactor 2.
В состав легких фракций нестабильного газоконденсата входят низкомолекулярные меркаптаны. Перед началом работы реактор 2 установки разогревается до температуры 350°С с помощью электронагревателей. После выхода реактора 2 в необходимый температурный режим включают насосы 17, 18 и начинается подача сырья в печь 1, где производится его нагрев за счет дизельной горелки (в момент запуска), подключенной к внешнему источнику дизельного топлива. Индикатором выхода установки в рабочий режим является постоянное выделение газа на свечу дожита и рост давления в реакторе 2 до рабочего. После этого происходит переход работы установки в режим работы подогрева сырья с The composition of light fractions of unstable gas condensate includes low molecular weight mercaptans. Before starting work, the reactor 2 of the installation is heated to a temperature of 350°C using electric heaters. After the reactor 2 reaches the required temperature, pumps 17, 18 are turned on and the feedstock is fed into the furnace 1, where it is heated by a diesel burner (at the time of start-up) connected to an external source of diesel fuel. The indicator of the output of the installation in the operating mode is the constant release of gas on the candle is lived out and the pressure in the reactor 2 rises to the operating one. After that, the operation of the installation switches to the mode of operation of heating the raw material with
ЗАМЕНЯЮЩИЙ ЛИСТ (ПРАВИЛО 26)
использованием газовой фазы, выделяемой на газосепараторе 11 из полученного в реакторе 2 катализата в процессе протекания реакции каталитического синтеза. SUBSTITUTE SHEET (RULE 26) using the gas phase separated in the gas separator 11 from the catalyzate obtained in the reactor 2 during the course of the catalytic synthesis reaction.
Сырье - прямогонная бензиновая фракция КК-210°С подается насосом 17 через фильтр 31 и рекуперативный теплообменник 16 в емкость накопления сырья 15 и далее насосом 18 прогоняется через систему рекуперативных теплообменников 13, 3, 4 и 5, где нагревается за счет тепла продуктов реакции до 200°С направляется в керосиновый сепаратор 12, в котором с верха сепаратора 12 газосырьевую смесь направляют через трубный теплообменник 6 в печь 1 для подогрева, а с низа сепаратора 12 собирают керосиновые фракции прошедшие через теплообменник 13 в емкость 14 для накопления керосина, которые в дальнейшем насосом 19 откачиваются с установки. Raw material - straight-run gasoline fraction KK-210°C is supplied by pump 17 through filter 31 and recuperative heat exchanger 16 into raw material storage tank 15 and then by pump 18 it is driven through a system of recuperative heat exchangers 13, 3, 4 and 5, where it is heated by the heat of reaction products to 200°C is sent to the kerosene separator 12, in which from the top of the separator 12 the gas mixture is sent through the pipe heat exchanger 6 to the furnace 1 for heating, and from the bottom of the separator 12 the kerosene fractions that have passed through the heat exchanger 13 are collected into the tank 14 for the accumulation of kerosene, which are further pump 19 is pumped out of the installation.
Из печи 1 подогретая газосырьевая смесь поступает в каталитический реактор 2, заполненный высококремнеземным цеолитсодержащим катализатором. Объемная скорость подачи сырья - от 4,5 до 5,0 литров в минуту. В реакторе 2 при температуре 350-450°С и давлении от 3,5 до 5 атм осуществляется процесс превращения низкооктановых компонентов прямогонной бензиновой фракции в высокооктановые за счет каталитической изомеризации и ароматизации парафиновых и дегидрирования нафтеновых углеводородов. From the furnace 1, the heated gas mixture enters the catalytic reactor 2 filled with a high-silica zeolite-containing catalyst. The volumetric feed rate of raw materials is from 4.5 to 5.0 liters per minute. In reactor 2 at a temperature of 350-450°C and a pressure of 3.5 to 5 atm, the process of converting low-octane components of straight-run gasoline fractions into high-octane ones is carried out due to catalytic isomerization and aromatization of paraffins and dehydrogenation of naphthenic hydrocarbons.
Реакционная смесь проходит с равномерным перепадом через трубопроводы реактора 2, в которых засыпан катализатор, где с прохождением характерных химических реакций, преобразующих углеводородный состав бензиновых фракций. Реакции протекают в одну ступень с поглощением тепла и выделением избыточного количества водородосодержащих газов (ВСГ). При этом происходит адсорбционная очистка газосырьевой смеси от сернистых соединений, которые остаются в реакторе и удаляются из него в момент регенерации (в процессе реакции каталитического окисления). The reaction mixture passes with a uniform drop through the pipelines of the reactor 2, in which the catalyst is filled, where with the passage of characteristic chemical reactions that transform the hydrocarbon composition of gasoline fractions. The reactions proceed in one step with the absorption of heat and the release of an excess amount of hydrogen-containing gases (HCG). In this case, the adsorption purification of the gas mixture from sulfur compounds occurs, which remain in the reactor and are removed from it at the time of regeneration (during the catalytic oxidation reaction).
Процесс осуществляется в неподвижном слое катализатора в режиме однократного пропускания, то есть без подачи рециклом потока ароматических соединений; олефиновый поток в основном расходуется в реакции. Используемый катализатор на основе цеолита, отличающийся от The process is carried out in a fixed catalyst bed in a single pass mode, that is, without the recycle flow of aromatic compounds; the olefin stream is mainly consumed in the reaction. The zeolite-based catalyst used, other than
ЗАМЕНЯЮЩИЙ ЛИСТ (ПРАВИЛО 26)
других катализаторов высокой активностью и высокой селективностью при длительном сроке службы катализатора в типичных рабочих условияхSUBSTITUTE SHEET (RULE 26) other catalysts with high activity and high selectivity with long catalyst life under typical operating conditions
Полученный катализат поступает обратно на циркуляцию в систему теплообменников 6, 5, 4, 3, и далее через 7, 8, 9, где охлаждается до температуры до 25°С, после чего через фильтр 32 катализата поступает в газосепаратор 11. The resulting catalyzate is fed back for circulation to the system of heat exchangers 6, 5, 4, 3, and then through 7, 8, 9, where it is cooled to a temperature of up to 25°C, after which it enters the gas separator 11 through the filter 32 of the catalyzate.
С верха газосепаратора 11 балансовый избыток углеводородного газа выводится с установки и используется в качестве топливного газа для печи 1. Катализат с низа газосепаратора 11 откачивается насосом 20 через теплообменник 16 в емкостной парк. From the top of the gas separator 11, the balance excess of hydrocarbon gas is removed from the plant and used as fuel gas for the furnace 1. The catalyzate from the bottom of the gas separator 11 is pumped out by the pump 20 through the heat exchanger 16 to the tank farm.
На выходе получен бензин катализа (т.к.30-208°С) (ОЧММ 74-80), который применяется как компонент для получения автомобильного бензина. At the output, catalysis gasoline (because 30-208 ° C) (OCMM 74-80) was obtained, which is used as a component for the production of motor gasoline.
Установка автоматически поддерживает параметры технологического режима на заданном уровне, регистрирует параметры и сигнализирует об отклонении параметров от заданных величин. The installation automatically maintains the parameters of the technological mode at a given level, registers the parameters and signals about the deviation of the parameters from the specified values.
Поддержание заданных параметров достигается за счет считывания контроллерами показаний с температурных датчиков, установленных в печи 1 и в реакторе 2, датчиков давления, установленных в реакторе 2, поплавковых датчиков, установленных в емкостях 14 и 15, расходомеров 28, 29, 30 и управления электромагнитными клапанами 21, 22 ,23 на трубопроводах установки. Maintaining the set parameters is achieved by reading controllers readings from temperature sensors installed in furnace 1 and reactor 2, pressure sensors installed in reactor 2, float sensors installed in tanks 14 and 15, flow meters 28, 29, 30 and control of electromagnetic valves 21, 22, 23 on the installation pipelines.
ЗАМЕНЯЮЩИЙ ЛИСТ (ПРАВИЛО 26)
SUBSTITUTE SHEET (RULE 26)
Claims
1. Установка каталитической переработки легких углеводородных фракций, содержащая последовательно связанные трубопроводами разогревающие сырье рекуперативные теплообменники (3, 4, 5), печь (1), каталитический реактор (2), а также охлаждающие катализат рекуперативные теплообменники (7, 8, 9), связанные с газосепаратором (11), выполненным с возможностью разделения катализата на газовую фазу, содержащую сероводород, и жидкую фазу, являющуюся конечным продуктом каталитической переработки, отличающаяся тем, что выход рекуперативных теплообменников (3, 4, 5) соединен с керосиновым сепаратором (12), выполненным с возможностью разделения разогретого сырья на газосырьевую смесь, предназначенную для последующего поступления в каталитический реактор (2) и керосиновую фракцию, при этом выход газовой фазы газосепаратора (11) связан трубопроводом с печью (1), а выход катализата из каталитического реактора (2) связан с рекуперативными теплообменниками (6, 5, 4, 3), которые связаны с охлаждающими рекуперативными теплообменниками (7, 8, 9). 1. Installation for the catalytic processing of light hydrocarbon fractions, containing recuperative heat exchangers (3, 4, 5) heating the raw materials, a furnace (1), a catalytic reactor (2), as well as recuperative heat exchangers (7, 8, 9) cooling the catalysate, connected in series with pipelines, associated with a gas separator (11) configured to separate the catalyzate into a gas phase containing hydrogen sulfide and a liquid phase, which is the final product of catalytic processing, characterized in that the outlet of the recuperative heat exchangers (3, 4, 5) is connected to a kerosene separator (12) , made with the possibility of separating the heated raw material into a gas mixture intended for subsequent entry into the catalytic reactor (2) and a kerosene fraction, while the gas phase outlet of the gas separator (11) is connected by a pipeline to the furnace (1), and the catalysate outlet from the catalytic reactor (2 ) is associated with recuperative heat exchangers (6, 5, 4, 3), which are associated with cooling river operational heat exchangers (7, 8, 9).
2. Установка каталитической переработки по п. 1, отличающаяся тем, что охлаждающие рекуперативные теплообменники (7, 8, 9) включают по меньшей мере один рекуперативный теплообменник, связанный с радиатором охлаждения, и по меньшей мере один рекуперативный теплообменник с водяным охлаждением. 2. Catalytic processing plant according to claim 1, characterized in that the cooling recuperative heat exchangers (7, 8, 9) include at least one recuperative heat exchanger connected to a cooling radiator and at least one water-cooled recuperative heat exchanger.
3. Установка каталитической переработки по п. 1, отличающаяся тем, что керосиновый сепаратор (12) связан через рекуперативный теплообменник (13) с емкостью (14) для сбора керосиновых фракций. 3. Catalytic processing plant according to claim 1, characterized in that the kerosene separator (12) is connected through a recuperative heat exchanger (13) to a container (14) for collecting kerosene fractions.
4. Установка каталитической переработки по п. 1, отличающаяся тем, что каталитический реактор (2) состоит по меньшей мере из двух реакторных колонн. 4. Catalytic processing plant according to claim 1, characterized in that the catalytic reactor (2) consists of at least two reactor columns.
5. Установка каталитической переработки по п. 1, отличающаяся тем, что на выходе жидкой фазы из газосепаратора (11) дополнительно установлен рекуперативный теплообменник. 5. Catalytic processing plant according to claim 1, characterized in that a recuperative heat exchanger is additionally installed at the outlet of the liquid phase from the gas separator (11).
ЗАМЕНЯЮЩИЙ ЛИСТ (ПРАВИЛО 26)
I I SUBSTITUTE SHEET (RULE 26) II
6. Установка каталитической переработки по и. 1, отличающаяся тем, что содержит температурные датчики, установленные в печи (1) и в каталитическом реакторе (2), датчики давления, установленные в каталитическом реакторе (2), поплавковые датчики, установленные в емкостях для сбора керосиновых фракций (14) и сырья (15), расходомеры, насосы и электромагнитные клапаны, установленные на трубопроводах установки и выполненные с обеспечением регулирования скорости прохождения рабочей среды. 6. Installation of catalytic processing for and. 1, characterized in that it contains temperature sensors installed in the furnace (1) and in the catalytic reactor (2), pressure sensors installed in the catalytic reactor (2), float sensors installed in tanks for collecting kerosene fractions (14) and raw materials (15), flow meters, pumps and solenoid valves installed on the pipelines of the plant and designed to control the speed of the passage of the working medium.
7. Способ каталитической переработки легких углеводородных фракций, осуществляемый в установке по и. 1, включающий нагрев сырья, контакт сырья с катализатором в каталитическом реакторе, охлаждение полученного катализата, последующее разделение катализата посредством газосепаратора (11) на газовую фазу, содержащую сероводород, и жидкую фазу, являющуюся конечным продуктом каталитической переработки, отличающийся тем, что подогретое посредством рекуперативных теплообменников (3, 4, 5) сырье предварительно разделяют с помощью керосинового сепаратора (12) на керосиновую фракцию и газосырьевую смесь, которую нагревают в печи (1) и направляют в каталитический реактор (2), после чего полученный катализат охлаждают посредством охлаждающих рекуперативных теплообменников (7, 8, 9), предварительно подавая его на циркуляцию в рекуперативные теплообменники (6, 5, 4, 3). 7. The method of catalytic processing of light hydrocarbon fractions, carried out in the installation according to and. 1, including heating of the feedstock, contact of the feedstock with the catalyst in the catalytic reactor, cooling of the obtained catalyzate, subsequent separation of the catalyzate by means of a gas separator (11) into a gas phase containing hydrogen sulfide and a liquid phase, which is the final product of catalytic processing, characterized in that it is heated by means of recuperative heat exchangers (3, 4, 5), the raw material is pre-separated using a kerosene separator (12) into a kerosene fraction and a gas feed mixture, which is heated in a furnace (1) and sent to a catalytic reactor (2), after which the resulting catalyzate is cooled by means of cooling recuperative heat exchangers (7, 8, 9), preliminary supplying it for circulation to recuperative heat exchangers (6, 5, 4, 3).
8. Способ каталитической переработки по п.7, отличающийся тем, что в качестве катализатора использован высококремнеземный цеолитосодержащий катализатор, для которого условиями для осуществления процесса пря ой конверсии являются температура от 350 до 450°С и давление от 3,5 до 5 атм, объемная скорость подачи сырья - от 4,5 до 5,0 литров в минуту. 8. The method of catalytic processing according to claim 7, characterized in that a high-silica zeolite-containing catalyst is used as a catalyst, for which the conditions for the implementation of the direct conversion process are temperature from 350 to 450 ° C and pressure from 3.5 to 5 atm, volumetric raw material feed rate - from 4.5 to 5.0 liters per minute.
9. Способ каталитической переработки по и.7, отличающийся тем, что в качестве топливного газа для печи (1) установки используют газовую фазу газосенаратора (11). 9. The method of catalytic processing according to item 7, characterized in that the gas phase of the gas generator (11) is used as the fuel gas for the furnace (1) of the plant.
ЗАМЕНЯЮЩИЙ ЛИСТ (ПРАВИЛО 26)
SUBSTITUTE SHEET (RULE 26)
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
RU2021113903A RU2753602C1 (en) | 2021-05-17 | 2021-05-17 | Method for catalytic processing of light hydrocarbon fractions and installation for its implementation |
RU2021113903 | 2021-05-17 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2022245253A1 true WO2022245253A1 (en) | 2022-11-24 |
Family
ID=77349387
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/RU2022/050116 WO2022245253A1 (en) | 2021-05-17 | 2022-04-01 | Process for catalytically converting light hydrocarbon fractions and apparatus for carrying out same |
Country Status (3)
Country | Link |
---|---|
CN (1) | CN114874808B (en) |
RU (1) | RU2753602C1 (en) |
WO (1) | WO2022245253A1 (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN118142484A (en) * | 2024-05-13 | 2024-06-07 | 东营联合石化有限责任公司 | Light hydrocarbon isomerization device and application method thereof |
Citations (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2067081A1 (en) * | 1969-11-10 | 1971-08-13 | Standard Oil Co | |
US3679575A (en) * | 1969-11-03 | 1972-07-25 | Standard Oil Co | Reforming with a platinum mordenite-alumina catalyst |
US4996381A (en) * | 1988-10-07 | 1991-02-26 | Mobil Oil Corp. | Increased conversion of C2 -C12 aliphatic hydrocarbons to aromatic hydrocarbons using a highly purified recycle stream |
US5030783A (en) * | 1989-01-17 | 1991-07-09 | Mobil Oil Corporation | Endothermic hydrocarbon upgrading process |
RU4746U1 (en) * | 1996-01-16 | 1997-08-16 | Акционерное общество открытого типа "Научно-исследовательский и проектный институт по переработке газа" | INSTALLATION OF CATALYTIC PRODUCTION OF HIGH-OCTANE GASOLINE FROM HYDROCARBON RAW MATERIAL |
RU2098173C1 (en) * | 1996-04-09 | 1997-12-10 | Инженерно-техническая фирма в форме товарищества с ограниченной ответственностью "Цеоконсалт" | Installation for catalytic production of high-octane gasoline fractions and aromatic hydrocarbons |
US5858209A (en) * | 1994-08-15 | 1999-01-12 | Uop | Catalytic reforming process with increased aromatics yield |
RU2152977C1 (en) * | 1998-12-10 | 2000-07-20 | Джабраил Джамал оглы Полатханов | Method of processing hydrocarbon raw material based on aliphatic hydrocarbons |
RU2175959C2 (en) * | 2000-01-21 | 2001-11-20 | Фалькевич Генрих Семенович | Method of processing aliphatic c2-c12-hydrocarbons into aromatic hydrocarbons or high-octane gasoline |
RU2181750C1 (en) * | 2001-04-19 | 2002-04-27 | Институт катализа им. Г.К. Борескова СО РАН | Method of processing petroleum distillates (options) |
Family Cites Families (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB632193A (en) * | 1947-01-10 | 1949-11-17 | Anglo Iranian Oil Co Ltd | Improvements relating to the catalytic cracking of petroleum hydrocarbons |
NL8104327A (en) * | 1981-09-21 | 1983-04-18 | Shell Int Research | PROCESS FOR PREPARING A HYDROCARBON MIXTURE |
US4450311A (en) * | 1983-06-29 | 1984-05-22 | Mobil Oil Corporation | Heat exchange technique for olefin fractionation and catalytic conversion system |
US5228978A (en) * | 1989-07-18 | 1993-07-20 | Amoco Corporation | Means for and methods of low sulfur and hydrotreated resids as input feedstreams |
US5500108A (en) * | 1991-08-15 | 1996-03-19 | Mobil Oil Corporation | Gasoline upgrading process |
JP2007270063A (en) * | 2006-03-31 | 2007-10-18 | Nippon Oil Corp | Method for treating light hydrocarbon composition, aromatic hydrocarbon composition, aromatic hydrocarbon, gasoline and naphtha |
CN100473712C (en) * | 2006-06-28 | 2009-04-01 | 中国石油集团工程设计有限责任公司抚顺分公司 | Technical flow of hydrogenation of gasoline through catalytic cracking full distillate |
CN101245260A (en) * | 2008-02-20 | 2008-08-20 | 宋金文 | Method for producing ultra-low-sulfur oil |
CN105647581B (en) * | 2014-11-12 | 2017-09-15 | 中国石油天然气股份有限公司 | catalytic gasoline hydrogenation method |
RU2658826C1 (en) * | 2017-08-04 | 2018-06-25 | Андрей Юрьевич Беляев | Motor fuel production method and installation |
CN109385301B (en) * | 2017-08-08 | 2021-01-01 | 中国石油天然气股份有限公司 | Hydrocarbon oil catalytic conversion method for light hydrocarbon and heavy hydrocarbon composite raw material |
-
2021
- 2021-05-17 RU RU2021113903A patent/RU2753602C1/en active
-
2022
- 2022-04-01 WO PCT/RU2022/050116 patent/WO2022245253A1/en active Application Filing
- 2022-05-10 CN CN202210503708.3A patent/CN114874808B/en active Active
Patent Citations (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3679575A (en) * | 1969-11-03 | 1972-07-25 | Standard Oil Co | Reforming with a platinum mordenite-alumina catalyst |
FR2067081A1 (en) * | 1969-11-10 | 1971-08-13 | Standard Oil Co | |
US4996381A (en) * | 1988-10-07 | 1991-02-26 | Mobil Oil Corp. | Increased conversion of C2 -C12 aliphatic hydrocarbons to aromatic hydrocarbons using a highly purified recycle stream |
US5030783A (en) * | 1989-01-17 | 1991-07-09 | Mobil Oil Corporation | Endothermic hydrocarbon upgrading process |
US5858209A (en) * | 1994-08-15 | 1999-01-12 | Uop | Catalytic reforming process with increased aromatics yield |
RU4746U1 (en) * | 1996-01-16 | 1997-08-16 | Акционерное общество открытого типа "Научно-исследовательский и проектный институт по переработке газа" | INSTALLATION OF CATALYTIC PRODUCTION OF HIGH-OCTANE GASOLINE FROM HYDROCARBON RAW MATERIAL |
RU2098173C1 (en) * | 1996-04-09 | 1997-12-10 | Инженерно-техническая фирма в форме товарищества с ограниченной ответственностью "Цеоконсалт" | Installation for catalytic production of high-octane gasoline fractions and aromatic hydrocarbons |
RU2152977C1 (en) * | 1998-12-10 | 2000-07-20 | Джабраил Джамал оглы Полатханов | Method of processing hydrocarbon raw material based on aliphatic hydrocarbons |
RU2175959C2 (en) * | 2000-01-21 | 2001-11-20 | Фалькевич Генрих Семенович | Method of processing aliphatic c2-c12-hydrocarbons into aromatic hydrocarbons or high-octane gasoline |
RU2181750C1 (en) * | 2001-04-19 | 2002-04-27 | Институт катализа им. Г.К. Борескова СО РАН | Method of processing petroleum distillates (options) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN118142484A (en) * | 2024-05-13 | 2024-06-07 | 东营联合石化有限责任公司 | Light hydrocarbon isomerization device and application method thereof |
Also Published As
Publication number | Publication date |
---|---|
CN114874808B (en) | 2023-10-17 |
CN114874808A (en) | 2022-08-09 |
RU2753602C1 (en) | 2021-08-18 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US10125322B2 (en) | Method for revamping a conventional mineral oils refinery to a biorefinery | |
Moulijn et al. | Chemical process technology | |
CN103814114B (en) | The fluid catalytic cracking paraffinic naphtha in downflow reactor | |
JP6267694B2 (en) | Direct catalytic cracking of crude oil by temperature gradient process | |
US9193919B2 (en) | Process for hydrodeoxygenation and process for upgrading of pyrolysis oil resulting from biomass, which are capable of operating continuously | |
US20110028573A1 (en) | High Shear Production of Value-Added Product From Refinery-Related Gas | |
WO2012000115A1 (en) | Method to upgrade heavy oil in a temperature gradient reactor (tgr) | |
US11286434B2 (en) | Conversion process using supercritical water | |
Larraz | A brief history of oil refining | |
WO2022245253A1 (en) | Process for catalytically converting light hydrocarbon fractions and apparatus for carrying out same | |
CN103228766B (en) | The conversion of Sweet natural gas | |
JPH0959652A (en) | Production of fuel oil base | |
CA2899133A1 (en) | System and process for thermal cracking and steam cracking | |
RU2567534C1 (en) | Method and device for obtaining of high-octane gasoline by combined processing of hydrocarbon fractions and oxygen-containing organic raw material | |
RU2098173C1 (en) | Installation for catalytic production of high-octane gasoline fractions and aromatic hydrocarbons | |
RU2213765C1 (en) | Installation for catalytic processing of light hydrocarbon material | |
Reinhardt et al. | Oxygen enrichment for intensification of air oxidation reactions. | |
RU38340U1 (en) | PLANT FOR PRODUCING C4-C6-ISOPARAFINS | |
SU378024A1 (en) | ||
RU2053013C1 (en) | Apparatus for catalytic obtaining of high-octane gasoline | |
CA3236232A1 (en) | Process for production of a low-aromatic hydrocarbon from pyrolysis oil | |
Murphree | Fluid Hydroforming | |
SU345690A1 (en) | METHOD FOR OBTAINING REACTIVE FUEL AND FUEL FOR SUPERSPEAR AIRPLANES | |
EA030309B1 (en) | Hydrocarbon raw material distillation method | |
EA039642B1 (en) | Method for oligomerization of c2-c10 olefins and complex unit for producing high-octane gasolines, diesel fractions or aromatic hydrocarbons from c1-c10 hydrocarbon fractions of various composition and oxygen-containing c1-c6 compounds using it |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 22805063 Country of ref document: EP Kind code of ref document: A1 |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
122 | Ep: pct application non-entry in european phase |
Ref document number: 22805063 Country of ref document: EP Kind code of ref document: A1 |